JPS605001A - Method and device for cooling high-temperature synthetic gas - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION [Technical Field of the Invention] The present invention relates to cooling systems and, more particularly, to removing solids from hot synthesis gas so that solids do not accumulate on equipment components during the course of the process. The present invention relates to a method for cooling high temperature synthesis gas while doing so.

[Background of the invention]

As is well known to those skilled in the art, 1200'F (649°C) is an adequate temperature for cooling any hot gas, especially when these gases contain particles including ash and charcoal. It is difficult to cool it down to a certain level. A typical example of such a gas is synthesis gas, which is produced by incomplete combustion of liquid or gaseous hydrocarbon fuels or solid carbonaceous fuels. The main components of such a mixture in the desired gas phase may include carbon oxide and hydrogen, with other gas phase components including nitrogen, carbon dioxide, and inert gases. Synthesis gas produced in this way typically contains non-gaseous (usually solid) components.
Contains. The non-gas components include mainly inorganic ash and carbon-containing charcoal, which is mainly organic.

The high solid content of the gas creates very severe problems. The syngas produced typically contains 94 pounds (64.1 g/m3) of solids per 1000 cubic feet (NTP) of dry gas (depending on the syngas feedstock). These solids can build up and block equipment unless removed.

In the past, it has been difficult to remove small solid particles containing ash, slag, or char from syngas.

It has been found that standard particles consisting of particle sizes as small as 5 microns or less become agglomerated (due to the presence of water-soluble components acting as interparticle binders). This mass typically contains about 1 part by weight of water-soluble components. These condensates accumulate in various parts of the device, typically narrow conduits, openings such as outlets, or narrow openings leading thereto. Therefore, unless some measure is taken to prevent the build-up, the equipment will become clogged and must be shut down after an unreasonably short period of operation.

[Summary of the invention]

One of the directed aspects of the present invention is a method for cooling high temperature synthesis gas, comprising: flowing the synthesis gas at an initial temperature downwardly through a first contact zone; flowing over a wall of a contacting zone to contact the downwardly descending synthesis gas, which is then cooled to form a cooled synthesis gas; downwardly descending the wall through a second contacting zone; flowing the cooled synthesis gas downwardly in contact with the film; spraying the downwardly descending cooled synthesis gas in the second contact zone with a cooling liquid to cause the downwardly descending further cooled synthesis gas to flow downwardly; forming a gas; the further cooled synthesis gas;
passing the cooling liquid in the third contact zone into a further cooled synthesis gas containing a reduced amount of solid content; passing the synthesis gas in contact with a stream of sprayed cooling liquid in a fourth contact zone to provide cooled purified synthesis gas; and recovering the cooled purified synthesis gas. are doing.

The high temperature synthesis gas applicable to the method of the invention may be synthesis gas produced by gasification of coal.

In a typical coal gasification process, finely ground raw coal to an average particle size of 20-500 microns, preferably 30-300 microns, e.g. 200 microns, is slurried with an aqueous medium, e.g. 80 weight section,
The slurry preferably contains 50-75% by weight of solids, for example 60% by weight. The aqueous slurry is then introduced into the combustion chamber. In this chamber, the slurry is brought into contact with an oxygen-containing gas (eg, air or oxygen) to cause incomplete combustion. The atomic weight ratio of oxygen to carbon within the device can be 0.7-1.2:1, for example 0.9:1.

A typical reaction is 1800'F-3500'F (982
°C to 1927 °C), for example 2500 °F (1371 °C
) and a temperature of 100-1500 psig (6,9 to 103 bars), preferably 500-1200
psig (35 to 83 bars), e.g. 9
It is carried out under a pressure of 0.00 psig (62 bar).

Alternatively, synthesis gas can be produced by incomplete combustion of hydrocarbon gases. Typical hydrocarbon gases include methane, which includes mixtures of light hydrocarbon feedstocks with a specific gravity of 1, or mixtures of liquid hydrocarbons such as fuel residues, asphalt, or solid carbonaceous materials. ,
There are ethane, propane, etc. The solid carbonaceous material includes coke from petroleum or tar sand asphalt),! Coke from blue or semi-bituminous coal, or
There are things like carbonaceous residues from coal and hydrogen combination processes, etc.

When using liquid, gaseous, or solid carbonaceous materials, equipment that can actually be used in the present invention includes, among others, gas generators such as those described in the following patents: U.S. Patent No. 2,818,326 Easttnan et al. U.S. Patent No. 2,896,927 Negl
Mr. E et al. U.S. Patent No. 3,998,609 C
Rouch et al. U.S. Patent No. 4, 218, 42
No. 3 Mr. Robin The effluent from the reaction zone where other feedstocks are gasified to produce synthesis gas is rated at 1500 psi.
g (6,9 to 103 bars), preferably 500
-1200 psig (35 to 83 bars), e.g. 900 psig (62 bars), 180
0'F - 3500'F (982 to 1927°C), preferably t L < Ha 2000'F - 2800'F (10
93 to 1538°C), e.g. 2500'F (137°C)
1°C).

Under these standard operating conditions, synthesis gas is typically (on a dry basis, 35-55 volumes, e.g. 50
Carbon monoxide by volume: 30-45 volume, e.g. 38 volume ratio Hydrogen: 10-20 volume ratio, e.g. 12 volume ratio Carbon dioxide: 0.3% by volume - 2 volume ratio, e.g. 0.8 volume ratio of hydrogen sulfide; 0.4-0.8 parts by volume, such as 0.6 parts by volume of nitrogen; and an amount of up to about 0.1 parts by volume of meth.

If the fuel is a solid carbonaceous material, the synthesis gas produced will typically be 100 cubic feet (N
TP)Naoshi, 1-1oPoy)' (16,1-161
g/m3, for example 4 bonds (64.1 g/m3) of solids (including ash, charcoal, slag, etc.).

These solids can exist in particle sizes from less than 1 micron to aooo microns. The material charcoal may contain ash in an amount of 0.5% by weight or more than 0.5% by weight.

This ash can be found in the syngas produced.

In the practice of the present invention, hot synthesis gas is flowed downwardly through the first contacting zone at the initial temperature described above. The upper end of the first contact zone is formed by the lower outlet portion of the reaction chamber of the gas generator. The first contact zone is formed entirely by an upright, preferably vertical peripheral wall. The peripheral wall is in the form of an elongated conduit. The cross-sectional shape of the zone defined by this wall is, in the preferred embodiment, #
The hill is cylindrical. The outlet or lower end of the narrow conduit or dip tube may be provided with a serrated edge at the lower end of the cylindrical wall.

The first contact zone may be bounded by the top of a vertically extending cylindrical dip tube. The dip pipes have a common axis with respect to the combustion chamber.

A cooling ring is attached to the upper end of the first contact zone of the dip tube. Through this ring, a cooling liquid, typically water, is introduced into the first contact zone. A first stream of coolant flows from the cooling ring along the inner wall of the dip tube.
A stream of water is poured out.

A preferably continuous downwardly flowing film of cooling liquid is formed on this inner wall. This coolant film is
It comes into contact with the syngas falling downward. Coolant inlet temperature is 100'F-5006F (38℃ to 260℃)
, preferably 3006F - 480'F (149°C to 249°C), for example below 420°C (216°C).

1000 cubic feet (NTP) of gas and 20-70 lbs (32 lbs) of coolant are introduced into the first contact zone.
0-1121 g/m, preferably 30=50 lbs (
481-801 g/ms), e.g. 45 lbs (7
A quantity of 21 g/m is added to the falling film on the wall of the dip tube. One of the features of the method according to the invention is that the cooling liquid introduced into the contact zone and, in turn, the cooling liquid introduced into the separation cooling ring contains recirculated liquid. This liquid has been treated to reduce its solid content. The liquid should contain less than about 0.1% by weight of solids having a particle size greater than about 100 microns. It is) 1 hydrocloning work (hydrocloning)
) makes it possible.

The falling film of coolant contacts the downwardly descending hot syngas, and the temperature of the hot syngas is 200'F-50.
Only 0°F (111 to 278°C), e.g. 350°F
(194°C). High-temperature synthesis gas is the first
This is because it comes into contact with the falling film while passing through the contact zone.

The gas may pass through the first contact zone for a period of 1-8 seconds, preferably for a period of 1-5 seconds, such as for a period of 3 seconds. The solid content of the gas leaving this zone may be reduced.

The cooled synthesis gas exiting the first contacting zone, which cools the synthesis gas with a falling film of coolant, is introduced into a second contacting zone. During venting of this zone, the cooled syngas is further brought into contact with the downwardly descending cooling liquid.

In the process according to the invention, in the second contact zone, a spray of cooling liquid is applied at 100°F-(38 to 260°C);
For example, at 420'F (216C), preferably at the top of the zone. This spray is directed in a direction perpendicular to the inner wall of the dip tube (ie, toward the axis of the dip tube). As the syngas passes through the second contact zone, the sprayed liquid and the descending syngas come into intimate contact, resulting in the same total amount of cooling liquid flowing downward as a wall film. In comparison, high levels of heat can be transferred multiple times, resulting in reliable cooling of the synthesis gas.

The amount of liquid sprayed into the second contact zone is equal to 1000 feet of dry gas (
NTP) (913g/h/m”) and about 20-80 bonds per hour (320 to 1281g/h/m”)
3), preferably time a, II) 30-60 bond (4
81 to 961 g/h/m, for example 57 pounds per hour (912 g/h/m3). Due to the high degree of contact between the gas and liquid, the temperature of the gas is reduced by 600°F - below 1300°C (333 to 722°C), preferably 800°C, while passing through the second zone. F-12006
F (444 to 667 C), for example 1100' F (
611°C).

The gas leaving the second contact zone thus contains a reduced concentration of solids.

The lower end of the second contact zone is immersed in a liquid pool of collected cooling liquid. The liquid level when considered as a static pool is typically 10-80% of the second welding zone.
For example, the water level can be maintained at a level where 50 people are submerged. It is clear to those skilled in the art that under the actual high temperature and high velocity gas, the liquid level during operation cannot be specified. Rather, the liquid is actively agitated.

The further cooled synthesis gas is, for example, 900'F-105
0! F (482 to 566 C) exiting the bottom of the second contact zone. The coolant liquid (constituting the third contact zone) is then passed through and over the lower grooves of the dip tube. The solids settle within the coolant liquid. Solids are retained within the coolant and can also be collected and removed by draining the liquid bottom of the coolant. Typically, the gas exiting the third contact zone contains 70% of the solids.
5% will be excluded. The temperature drop of the gas as it passes through the third contact zone is 200-650°F (93-343°C
), for example, 350'F (177°C).

The further cooled gas at below 400'F -700 (204 to 371°C), e.g. It is also preferred to flow upwardly through the fourth contact zone in the direction of the gas outlet of the cooling chamber, preferably through an annular passage. In a preferred embodiment, the annular passageway is formed by the outer surface of the dip tube forming the first and second cooling zones and the inner surface of the container. The inner surface of the container is characterized by surrounding the dip tube and having a radius larger than the radius of the dip tube. While the gas passes upwardly through the fourth cooling zone, a water-like cooling liquid is sprayed onto the upwardly flowing gas. 20-70 bond per 1000 cubic feet (NTP) of dry gas (320 to 1121 g/m
For example, 40 bonds (640 g/m of liquid,
It may be introduced at 100'F-500'F (38 to 260°C), such as 420'F (216°C). The gas leaving the third contact zone is 1000 cubic feet (N
TP) contains 90.1-3 bonds (1,6 to 48 g/m) of solids per dry gas, e.g. 0.6 bonds (9,6 g/m), i.e. About 80-90% of the material is removed, e.g. 85% by weight.

A mixture of coolant and further cooled synthesis gas (400〒-
700''F (204 to 371C), e.g. 600''
F (inlet temperature of 316 °C)) passes upwardly through the annular fourth cooling zone, within which the two-phase flow facilitates efficient heat transfer from the hot gas to the coolant. Let's do it. Vigorous agitation within this fourth cooling zone minimizes the accumulation of particles on the contact surfaces. - As an example, the cooled gas is 300'F - 520°l''
(149 to 271°C), preferably 350'F-50
0°F (177 to 260°C), such as 450°F (2
At a temperature of 32° C., this annular fourth cooling zone is not exited. The gas leaving the fourth contact zone is 1000 cubic feet (NTP) of gas per meter, 0.1-2.5 bonds (1.6 to 40.3 g/m, e.g. 0.4 lbs.
It has a solid content of 6.4 g/m. That is, about 85-954, say 90%, of the solids are removed from the gas.

A feature of the present invention is that the cooled output gas, including synthesis gas and cooling liquid, is flowed (depending on the velocity head of the flow) toward the outlet of the cooling tube chamber and from there into the outlet conduit. Preferably, the outlet conduit is oriented radially with respect to the outer periphery of the shell surrounding the combustion chamber and the cooling chamber.

In carrying out the process according to the invention, it is possible to apply a directional cooling liquid or spray to the flow of the synthesis gas at the point where it enters the outlet conduit or outlet nozzle and leads from the cooling chamber to the venturi cleaning device. It is being done. In a preferred embodiment, the directional flow or spray of coolant is directed from an axial position of the outlet nozzle to
It is oriented along its axis towards the nozzle and venturi. Preferably, the venturis are installed on the same axis.

This stream provides some additional cooling to the synthesis gas, but
It has been found that there is an advantage in minimizing and removing rock solid build-up within the outlet nozzle and venturi cleaning system.

The solids deposits are caused by syngas-sourced ash and charcoal and cannot be completely removed by contact processing in some contact zones. This final directed liquid flow, e.g. 420"F (216°C)
．． It is preferable to add 6 g/m, for example 11 bond (176 g/m).

The coolant can be discharged from the lower part of the cooling chamber as used coolant. The discharged coolant contains hardened ash and charcoal in the form of small particles. If necessary, excess coolant can be added to and/or removed from a coolant reservoir in the lower part of the cooling chamber.

It is clear that this sequence of operations is characterized by its ability to remove the bulk of the solids (ash, slag, and charcoal) particles. Unless the solid particles are removed, the buildup will accelerate and the equipment will become clogged and clogged. It was also found that each cooling (washing) operation cooled the solids more efficiently and prevented water from evaporating from the surface of the particles carried by the gas in the gas outlet piping. ing. Evaporation of water concentrates the soluble solids contained in the water and these soluble solids reach a state of supersaturation, which acts undesirably as a binding promoter.

These water-soluble solids are dissolved by the respective water streams from the solids.

Each cooling and washing step ensures that fine ash particles are moistened and thus removed from the gas.

〔Example〕

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings.

This will be explained with reference to FIG. In this example, a reaction vessel 11 with a refractory lining 12 and an inlet nozzle 13 is provided. The reaction chamber 15 has an outlet section 14 with a narrow passage area 16 .

Said passage area 16 adjoins an opening 17 . The opening 17 opens into a first contact sea 718 inside the dip tube 21 . The tip of the dip tube 21 with serrations 23 is immersed in a bath 22 of coolant. Cooling room 19
is equipped with a gas exhaust conduit 20, preferably in its upper part.

A cooling ring 24 is mounted below the floor 25 at the top of the reaction vessel 11 . This cooling ring has an upper surface 26
It is equipped with This surface preferably contacts the lower part of the floor 25. Preferably, the lower surface 2T of the cooling ring rests on the upper end of the dip pipe 21. Cooling ring inner surface 28
is adjacent to the green of the opening 17. In the preferred embodiment, cooling ring 24 includes inlet nozzles 32 and 33.

The cooling ring 24 is equipped with an outlet nozzle 29 . These outlet nozzles may be in the form of a series of holes or nozzles around the periphery of the cooling ring 24 and located in close proximity to the inner surface of the dip tube 21. Passage or nozzle 29
The jetting liquid flows in a direction parallel to the axis of the dip pipe 21 and forms a thin falling film of cooling liquid that descends on the inner surface of the dip pipe 21. This falling film of coolant forms the outer boundary of the first contact zone.

A second contact seam 73 is attached to the lower end of the first contact seam 718.
There is 0. This second contact zone is because the tooth 23
The boundary is defined by a film of cooling liquid that extends downwardly toward the inside of the dip tube 21 and flows downwardly inside the dip tube 21. Within the boundaries of the second contact zone 3° there is a spray chamber (or ring) 31 with an outlet nozzle 35. The outlet nozzle is in the form of a series of holes or nozzles in the inner circumference of the chamber 31. The liquid ejected through the schematically represented spray nozzle 35 flows in a direction with a substantial component towards the axis of the dip tube 21 . In a preferred embodiment, the spray nozzles can be arranged circularly in the cooling ring, with the dip tube axis toward which they are oriented. Cooling liquid can be introduced into the spray chamber 31 through piping 33 .

In a second contact zone, characterized in that a spray is applied from the spray chamber 31, a further cooled synthesis gas is formed. This synthesis gas is passed downwardly into a third contacting zone substantially bounded by bath 22. The gas passes downwardly through the serrations 23 and then rises through the cooling liquid forming the third contact zone.

At the upper end of the third contact zone, the further cooled cooling gas containing a small amount of solids flows into the fourth zone 34.

The fourth contact zone is characterized by the addition of a spray stream of cooling liquid. The cooling liquid is introduced via piping 36 into a spray ring 40 from which the liquid is sprayed through nozzles 38.

The cooled output synthesis gas flows upwardly and is removed from the outlet nozzle 20. From this outlet nozzle it is preferably passed through a Venturi cleaning device to further remove solids. In this embodiment, liquid spray means may be provided. This means extends from the axis of the gas outlet nozzle 20, along the axis, into the nozzle 20 and into the venturi cleaning device.

(a venturi cleaning device preferably installed immediately after this nozzle) is adapted to eject a cooling liquid 39. This makes it possible to minimize the accumulation of solids at this location in the device.

In the process of the present invention using the apparatus of FIG. 1, 100 parts (all parts by weight unless otherwise specified) of feedstock carbonaceous fuel and 60 parts of feedstock carbonaceous fuel are added per unit time through the inlet nozzle 13. A slurry containing water is introduced. The slurry in this example has the following characteristics.

Ingredients Weight % Carbon 43.1 Hydrogen 3.5 Nitrogen 1.2 Sulfur 2.4 Oxygen 3.5 Inorganics 8.8 Water 37.5 Total 100 In addition, 90 parts of oxygen with a purity of 99.5 by volume was introduced. There is. Combustion in chamber 15 produces 900 psig (6
3 bara) to a temperature of 2500°F (1371°C). The synthesis gas passing through the outlet section 14 and narrow passage area 16 contains the following gas components: CO38,648,5 H2030,538 CO29.6 12 H2020- H2SO,81 N20.4 0.5 CH40 ,080,01.

In addition, this synthesis gas is 100O8CF dry gas (N
TP) may also contain approximately 4.1 pounds (66 g/m3) of solids.

The output synthesis gas (235 parts) exits narrow passage section 16 and flows through opening 1T in cooling ring 24 and into first contact seam 718 . Watery 4206F (216℃)
of cooling fluid is introduced into the ring 24 through the inlet pipe 34. The cooling liquid exits this ring 24 through an outlet nozzle 29 and forms a downwardly flowing film on the inner surface of the dip tube 21 which formed the outer boundary of the first contact zone 18 .

The syngas enters the first contact zone at about 2500'F (1371°C) and reaches about 21506F as it contacts the aqueous falling film and passes downwardly through zone 18.
(1177°C).

The synthesis gas thus cooled is then introduced into the second contacting zone 30. This zone is characterized by the addition of a coolant spray.

Cooling fluid is passed through coolant inlet piping 33 to a temperature of 420°F (
2t5t) into the second contact zone. This liquid flows into the spray passage 31. This spray passage has the unique shape of a circumferential distribution ring. From this ring, coolant is sprayed through holes in the wall of the dip tube 21 into the interior of the dip tube 21 forming a second cooling zone.

Within this second contact zone, the cooled syngas contacts both the sprayed coolant and the falling film as described above and is cooled to 1100'F (539C).

This further cooled synthesis gas is passed through the liquid of bath 22 in the third contacting zone. The drawing shows a static view with a sketchy water surface, but during operation, gas passes downward through the liquid, passes through the serrated edge 23 of the dip tube 21, and flows through the dip tube 21. It is clear that the gas and liquid are in a highly turbulent state as they pass upwardly through the liquid outside the tube 21.

The further cooled synthesis gas loses at least a portion of the solid content it contains while in contact with the cooling liquid.

Typically, further cooled syngas (600'F (3166C)) containing reduced ash particle content is
008CF dry gas (NTP) containing approximately 0.6 g/m of solids (including ash and charcoal).

The further cooled syngas containing reduced solids particle content is passed through a fourth cooling or contacting zone. Within this zone, the gas (316°C) is 420'F
(216° C.)” coolant spray.

Coolant (100O8CF dry gas (NTP))
0 lb (641 g/m3)) is introduced into the spray ring 40 through the coolant inlet 36. The ring is sprayed with its cooling liquid through a nozzle 38 into the fourth contact zone 34 . The cooled output syngas exits the fourth contact zone at 460'F (238C).

Cooling water can be drained through pipe 41 and collected solids can be removed through pipe 3T.

Exhaust gas is removed from the cooling device through exhaust conduit 20. This exhaust gas then typically passes through a venturi. At this time, it may be further mixed with a cooling liquid in order to contain supplementary cooling liquid and/or water. This venturi is preferably located close to the exit nozzle.

In a preferred embodiment, a spray 39 of aqueous coolant is added to the cooled syngas. Preferably, the spray is directed along the axis of the gas exhaust conduit and into the conduit. This serves to minimize or remove the build-up of solid particles within the conduit and the venturi immediately adjacent to the conduit.

FIG. 2 illustrates a process flow embodying the apparatus of FIG. 1, along with ancillary equipment that may be used in a preferred embodiment.

Synthesis gas (2
35 parts) at 460°F (238°C), 900p
sig (63 bar) and exits the cooling chamber through the gas exhaust conduit (outlet nozzle) 20. Dry gas 10
0.4 lb (6,1 g/m) per 0O8CF (NTP)
3) This syngas stream containing solids in the amount of
0 and is passed through a venturi mixer 51. In the venturi mixer, the syngas stream is contacted at 430° F. with 90 parts of 10008 CF dry gas (1441 g/m) of aqueous cooling liquid from line 52.

The flow (232° C.) in the pipe 5j is passed through a cleaning device (scrubber) 54. Here, the synthesis gas is 1000S
Per CF dry gas, 915.3 parts (245.1 g/m3
) is brought into contact with an aqueous cleaning liquid introduced from piping 55. As the synthesis gas from line 53 exits upwardly through a cleaning device 54 containing a vessel, tray or spray nozzle, the solid content is removed at a concentration of 0.4 Bond (6.1 g/m) per 100 O8 CF of dry gas. is decreased from the initial value of
Temperature is 229 below 885 paig (62 bars)
The temperature drops to ℃. In this state, synthesis gas is taken out through pipe 56.

The cleaning liquid (9200 pounds per 10008 CF dry gas (3204 g/m3)) exits the cleaning device 54 through line 57 at 229°C and passes through pump 58 and line 59. A part of it (calsM amount %) is recirculated to the venturi 51 through the pipes 60 and 52.

Replenishment water quality liquid is supplied to pipes 62, 63 and 64 as necessary.
It can also be supplied to the equipment through.

In order to flow through the piping 32 and then to the cooling ring 24,
The aqueous fluid stream being recirculated within piping 61 is treated to reduce its solid content. Typically, the flow in line 61 is 18 pounds per 100 cubic feet of liquid.
8g/m3) Contains solid matter (ash and charcoal). These solids are made up of particles with a size of 100 microns or more. Typically, the flow in line 61 can contain about 10 g/m of solids per 100 cubic feet of liquid, and these solids range from 1-5 microns in size to 200- It has been determined that the particles may be in the size range of 500 microns.The flow in line 61 is treated to separate large size particles.Particles larger than about 15 microns are removed. In a preferred mode of operation, this stream is treated such that at least 80% by weight of the particles remaining in stream 61 consist of particle sizes of about 10 microns or less. contains 0.03% by weight of solids.

This can be done by passing it through a filter, passing it through a bed of sand, or pouring it from a settling tank.
It is effective and preferable to perform this in a hydroelone 65. From this hydroclone, the ash-rich stream is removed through line 66.

When operated in this preferred manner, it has been observed that the outlet holes of the cooling ring remain free of deposits for extended periods of time.

[Brief explanation of the drawing]

FIG. 1 is a schematic vertical sectional view showing a generator and a cooling chamber attached thereto, and FIG. 2 is a schematic diagram showing a process flow plan as a preferred embodiment of the process of the present invention. -11... Reaction container, 12φ... Fireproof lie -'-
'gu, 13...Kenjin nozzle, 14...Exit part, 15...Reaction chamber, 16...Narrow passage part, 1
7... Opening, 18... First contact zone, 19
...Cooling room, 2o...Gas exhaust pipe, 21...
- Dip pipe, 22 Bath, 23 Serrated projection, 24 Cooling ring, 25 Life Floor, 2
6...Top surface, 27...Bottom surface, 28...Inner surface, 29...Outlet nozzle (exit passage), 30...
Second contact zone, 31...spray chamber (ring)
, 32.33... Inlet nozzle (piping), 34...
- Fourth inoculation zone, 35... Outlet nozzle, 36
...Piping, 37.38...Nozzle, 39.11
Ya・Spraying, 40-... Spraying, 41...
...Piping, 51...Venturi mixer, 54...
-Cleaning device, 58...Pump, 65II...Hydroclone. Patent Applicant: Texaco Development Φ Corporation Agent Masaki Yamakawa (and 2 others)

Claims (3)

[Claims] (1) In a method of cooling high temperature synthesis gas by cooling the high temperature synthesis gas with a cooling fluid in a series of contact zones; directing the synthesis gas at an initial temperature through a first contact zone; flowing a cooling fluid downwardly in a film on the walls of said first contact zone in contact with said downwardly descending syngas; through a second contact zone; flowing the cooled synthesis gas downwardly while contacting the downwardly descending film against the walls of the contact zone of 2;
further cooling the synthesis gas by spraying a cooling liquid onto the cooled synthesis gas descending downwardly in the second contact zone; passing the further cooled synthesis gas containing reduced solid content through a liquid; passing the further cooled synthesis gas containing reduced solid content into a sprayed cooling liquid; A method for cooling high-temperature synthesis gas, comprising the steps of: flowing through a fourth contact zone while being in contact with a flow; and recovering the cooled output gas of the synthesis gas. (2) High temperature synthesis gas containing solid particles including ash and charcoal was heated to 1800-3500'F (982-1927°C)
) to an initial high temperature of approximately 400-700°F (204-3
in a method of cooling to a final temperature of 71° C.); flowing an initially hot syngas containing ash and charcoal downward through a contact zone; flowing a cooling liquid containing solid particles below the weight ratio into said contact zone; passing the hot gas to a cooled synthesis gas; passing the cooled synthesis gas through a liquid coolant to produce a cooled output synthesis gas containing a reduced amount of solid particles; contacting the produced synthesis gas with a spray of an aqueous cleaning liquid to form a produced synthesis gas substantially free of solids and a cleaning effluent containing solid particles; At least a part of the solid particles are separated from at least a part of the washing waste liquid, and about 1
and flowing at least a portion of the liquid into the contact zone as at least a portion of the cooling liquid. A method for cooling high-temperature synthesis gas, comprising the steps of: (3) In a cooling device containing an axial dip tube assembly: a thin dip tube having inner and outer circumferential surfaces, an axis, and an inlet end and an outlet end; a cooling ring adjacent the surface and having a liquid inlet; on the cooling ring adjacent the inlet end of the dip tube and adapted to direct a curtain of fluid toward the outlet end of the dip tube; a first fluid outlet located intermediate the inlet end and the outlet end of the dip tube;
a first spraying means for directing the flow of liquid away from the inner peripheral surface of the dip tube and towards the axis of the dip tube; intermediate the inlet end and the outlet end of the dip tube;
a second spraying means for directing a stream of liquid onto the outer circumferential surface of the dip tube;
a first coolant spray in a second contact zone inside said dip tube and a third spray adjacent to the lower end of said dip tube.
and a spray of a second cooling liquid in a fourth contact sea/outside of the dip tube and then to a cooling gas outlet of said cooling device. A cooling device characterized by: